US5871560A - Process and plant for the direct reduction of iron-oxide-containing materials - Google Patents

Process and plant for the direct reduction of iron-oxide-containing materials Download PDF

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Publication number
US5871560A
US5871560A US08/765,342 US76534297A US5871560A US 5871560 A US5871560 A US 5871560A US 76534297 A US76534297 A US 76534297A US 5871560 A US5871560 A US 5871560A
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United States
Prior art keywords
gas
reducing
duct
direct reduction
iron
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Expired - Fee Related
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US08/765,342
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English (en)
Inventor
Roland Fluch
Karl Czermak
Gunter Peer
Roy Hubert Whipp, Jr.
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YOEST-ALPINE INDUSTRIEANLAGENBAU A CORP OF AUSTRIA GmbH
Primetals Technologies Austria GmbH
Brifer International Ltd
Original Assignee
Voest Alpine Industrienlagenbau GmbH
Brifer International Ltd
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Assigned to YOEST-ALPINE INDUSTRIEANLAGENBAU GMBH, A CORP. OF AUSTRIA, BRIFER INTERNATIONAL LTD., A CORP. OF BARBADOS reassignment YOEST-ALPINE INDUSTRIEANLAGENBAU GMBH, A CORP. OF AUSTRIA ASSIGNMENT OF ASSIGNORS INTEREST (SEE DOCUMENT FOR DETAILS). Assignors: CZERMAK, KARL, FLUCH, ROLAND, PEER, GUNTER, WHIPP, ROY HUBERT, JR.
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    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21B—MANUFACTURE OF IRON OR STEEL
    • C21B13/00—Making spongy iron or liquid steel, by direct processes
    • C21B13/0073—Selection or treatment of the reducing gases
    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21B—MANUFACTURE OF IRON OR STEEL
    • C21B2100/00—Handling of exhaust gases produced during the manufacture of iron or steel
    • C21B2100/20—Increasing the gas reduction potential of recycled exhaust gases
    • C21B2100/22—Increasing the gas reduction potential of recycled exhaust gases by reforming
    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21B—MANUFACTURE OF IRON OR STEEL
    • C21B2100/00—Handling of exhaust gases produced during the manufacture of iron or steel
    • C21B2100/20—Increasing the gas reduction potential of recycled exhaust gases
    • C21B2100/28—Increasing the gas reduction potential of recycled exhaust gases by separation
    • C21B2100/282—Increasing the gas reduction potential of recycled exhaust gases by separation of carbon dioxide
    • C—CHEMISTRY; METALLURGY
    • C21—METALLURGY OF IRON
    • C21B—MANUFACTURE OF IRON OR STEEL
    • C21B2100/00—Handling of exhaust gases produced during the manufacture of iron or steel
    • C21B2100/60—Process control or energy utilisation in the manufacture of iron or steel
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P10/00—Technologies related to metal processing
    • Y02P10/10—Reduction of greenhouse gas [GHG] emissions
    • Y02P10/122—Reduction of greenhouse gas [GHG] emissions by capturing or storing CO2
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P10/00—Technologies related to metal processing
    • Y02P10/10—Reduction of greenhouse gas [GHG] emissions
    • Y02P10/134—Reduction of greenhouse gas [GHG] emissions by avoiding CO2, e.g. using hydrogen
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P10/00—Technologies related to metal processing
    • Y02P10/10—Reduction of greenhouse gas [GHG] emissions
    • Y02P10/143—Reduction of greenhouse gas [GHG] emissions of methane [CH4]

Definitions

  • the invention relates to a process for the direct reduction of iron-oxide-containing material, wherein synthesis gas, preferably reformed natural gas, is mixed with top gas forming in the direct reduction of the iron-oxide-containing material and is used as a reducing gas for direct reduction and for heating the iron-oxide-containing material to reduction temperature, as well as a plant for carrying out the process.
  • synthesis gas preferably reformed natural gas
  • Metal dusting occurs to an increased extent at elevated temperatures, plant parts that get into contact with hot reducing gas, thus, being particularly jeopardized. With a plant for carrying out the initially mentioned process, these are primarily the reactors employed for direct reduction and the gas heaters heating the reducing gas to reduction temperature.
  • the invention aims at avoiding these disadvantages and difficulties and has as its object to provide a process of the initially defined kind and a plant for carrying out the process, which enables the adjustment of the content of H 2 S to a predetermined value with sufficient accuracy and by avoiding great procedural and structural expenditures as well as high costs.
  • this object is achieved in that at least a portion of the sulfur contained in the iron-oxide-containing material, together with the top gas, is fed to the reducing gas in the form of H 2 S incurring in heating and in direct reduction, respectively.
  • the invention is based on the idea to utilize the sulfur usually contained in the ore and which has not been used in further processing so far, taking advantage of the fact that H 2 S is formed when heating sulfide ores. According to the invention, this H 2 S, together with the reducing gas effecting heating and by which it is absorbed, is carried off as a top gas and fed to the reducing gas.
  • a content of H 2 S ranging from 20 to 40 ppmV, preferably amounting to about 25 ppmV, is adjusted in the reducing gas by means of the top gas.
  • the top gas is subjected to CO 2 scrubbing prior to being used as a reducing gas and the adjustment of the H 2 S content in the reducing gas is effected by directly admixing to the reducing gas at least a partial volume of the top gas while avoiding CO 2 scrubbing.
  • This variant is particularly simple to realize, because the only thing to be provided is a bypass duct bypassing the CO 2 scrubber. Thereby, washing out of the H 2 S present in that portion of the top gas is prevented, whereas the remaining portion of the top gas is subjected to CO 2 scrubbing, by which also H 2 S is washed out.
  • the desired H 2 S content of the reducing gas may be adjusted in a simple manner.
  • Another preferred embodiment is characterized in that reformed natural gas is employed as the synthesis gas and that both the reformed natural gas and the top gas are subjected to CO 2 scrubbing prior to being used as a reducing gas, wherein a partial volume of the reformed natural gas is directly admixed to the reducing gas while avoiding CO 2 scrubbing.
  • any desired CO 2 content may be adjusted in a simple manner and changes in the CO 2 content and in the CO/CO 2 ratio of the reducing gas caused by the direct admixture of a portion of CO 2 -unscrubbed top gas may be balanced out under consideration of the desired H 2 S content.
  • Another preferred way of adjusting the desired H 2 S content in the reducing gas is characterized in that the adjustment of the H 2 S content in the reducing gas is effected by varying the wash-out degree of CO 2 scrubbing with a view to retaining a portion of the CO 2 and hence a portion of the H 2 S in the scrubbed gas.
  • This embodiment requires the least structural expenditure possible, i.e., not even the arrangement of a bypass duct, yet it has to be taken into account that all of the gas must be conducted through the CO 2 scrubber, which will have to be dimensioned accordingly.
  • a sulfurous material such as iron pyrite
  • iron pyrite is added to the particulate iron-oxide-containing material in case it does not contain any sulfur, thus causing the formation of H 2 S and its absorption by the reducing gas effecting heating of the iron-oxide-containing material to reduction temperature.
  • a plant for carrying out the process comprising at least one direct reduction reactor for receiving the iron-oxide-containing material, heating and reducing the same, a reducing-gas supply duct leading to said direct reduction reactor and a top-gas discharge duct carrying off the direct reduction reactor the top gas forming in direct reduction as well as in heating to reduction temperature, the top-gas discharge duct running into a CO 2 scrubber and the reducing gas formed of synthesis gas and of top gas getting into the direct reduction reactor through the reducing-gas supply duct and the reducing-gas supply duct leading from the CO 2 scrubber to the direct reduction reactor, is characterized in that the top-gas discharge duct is flow-connected with the reducing-gas supply duct by means of a bypass duct avoiding the CO 2 scrubber.
  • a reformer for reforming natural gas and a reformed-gas duct departing from the reformer and joining the top-gas discharge duct are provided for the production of synthesis gas, both the reformed-gas duct and the top-gas discharge duct running into the CO 2 scrubber.
  • the reformed-gas duct is flow-connected with the reducing-gas supply duct by means of a bypass duct avoiding the CO 2 scrubber.
  • bypass duct(s) is (are) equipped with a adjustment valve, preferably a control valve, capable of being activated via an H 2 S measuring means.
  • a adjustment valve preferably a control valve
  • the FIGURE shows the plant according to the invention.
  • This plant comprises four whirl layer reactors 1 to 4 consecutively connected in series, wherein iron-oxide-containing material, such as fine ore, through an ore supply duct 5 is supplied to the first whirl layer reactor 1, in which heating to reduction temperature (or prereduction) takes place, and subsequently is conducted from one whirl layer reactor to another whirl layer reactor via conveying ducts 6.
  • the completely reduced material (sponge iron) is hot-briquetted in a briquetting arrangement 7. If required, the reduced iron is protected from reoxidation during briquetting by an inert gas system not illustrated.
  • Reducing gas is conducted in counterflow to the ore flow from one whirl layer reactor 4 to another whirl layer reactor 3 to 1 and is carried off the last whirl layer reactor 1, viewed in the gas flow direction, as a top gas through a top-gas discharge duct 8 and is cooled and scrubbed in a wet scrubber 9.
  • the production of reducing gas is effected by reforming in a reformer 10 natural gas fed through a duct 11 and desulfurized in a desulfurization plant 12.
  • the gas leaving the reformer 10 and formed of natural gas and vapor essentially consists of H 2 , CO, CH 4 , H 2 O and CO 2 .
  • This reformed natural gas is supplied through a reformed-gas duct 13 to several heat exchangers 14, in which it is cooled, water thus being condensed out of the gas.
  • the reformed-gas duct 13 runs into the top-gas discharge duct 8 after the top gas has been compressed by means of a compressor 15.
  • the mixed gas thus forming is passed through a CO 2 scrubber 16 and is freed from CO 2 and also from H 2 S. It is then available as a reducing gas.
  • This reducing gas via a reducing-gas supply duct 17, is heated to a reducing-gas temperature of about 800° C. in a gas heater 18 arranged to follow the CO 2 scrubber 16 and is fed to the first whirl layer reactor 4, viewed in the gas flow direction, where it reacts with the fine ores to produce directly reduced iron.
  • the whirl layer reactors 4 to 1 are arranged in series; the reducing gas gets from one whirl layer reactor to another whirl layer reactor through connection ducts 19.
  • a portion of the top gas is sluiced out of the gas circulatory system 8, 17, 19 in order to avoid enrichment of inert gases, such as N 2 .
  • the sluiced-out top gas is fed through a branch duct 20 to the gas heater 18 for heating the reducing gas and is burnt there. Possible shortages of energy are supplemented by natural gas supplied through a feed duct 21.
  • the sensible heat of the reformed natural gas emerging from the reformer 10 as well as of the reformer smoke gases is utilized in a recuperator 22 to preheat the natural gas after passage through the desulfurization plant 12, to produce the vapor required for reformation and to preheat the combustion air supplied to the gas heater 18 through duct 23 as well as, if desired, also the reducing gas.
  • the combustion air supplied to the reformer through duct 24 is preheated as well.
  • the top gas leaving the whirl layer reactor 1 has an H 2 S content ranging between 40 and 140 ppmV-depending on the sulfur content of the ore.
  • the H 2 S gas forms during heating of the fine ore to reduction temperature or during the prereduction of the fine ore, respectively.
  • H 2 S no longer is completely washed out of the top gas by means of the CO 2 scrubber, but it is taken care that the percentage of H 2 S desired for the reducing gas be fed to the reducing gas from the top gas.
  • this can be realized by means of a bypass duct 25 bypassing the CO 2 scrubber 16, which bypass duct departs from the top-gas discharge duct 8 via an adjustment or control valve 26 and runs into the reducing-gas supply duct 17.
  • the adjustment or control valve 26 is adjustable in a manner that an H 2 S content ranging between 20 and 40 ppmV, preferably amounting to about 25 ppmV, is H 2 S present in the reducing gas.
  • the adjustment or control valve 26 is activated via an H 2 S measuring means 27.
  • the desired H 2 S content in the reducing gas may be adjusted also by passing the total top gas through the CO 2 scrubber 16, yet adjusting the latter to a wash-out level at which a portion of the CO 2 and hence also a portion of the H 2 S will remain in the gas emerging from the CO 2 scrubber 16.
  • This has the advantage that no auxiliary means, such as a bypass duct 25 including a control valve 26, need be provided, yet requires the total gas amount, i.e. all of the top gas and all of the reformed natural gas, to be passed through the CO 2 scrubber 16, the latter, thus, having to be dimensioned for such an amount.
  • a portion of the reformed natural gas may be supplied to the reducing-gas supply duct 17 through a bypass duct 29 bypassing the CO 2 scrubber 16 and likewise equipped with an adjustable valve 28; that bypass duct 29 will then depart from the reformed gas duct 13.
  • the measures pointed out above for adjusting a desired H 2 S content in the reducing gas may be realized individually or also jointly.
  • the fine ore has the following analysis:
  • the reformed natural gas and the top gas have the chemical compositions indicated in the Table below.
  • the gas mixture emerging from the CO 2 scrubber 16 and formed of the scrubbed reformed natural gas and of the scrubbed top gas has the following composition:
  • This gas mixture is mixed with 78,000 Nm 3 /h of top gas that has not been passed through the CO 2 scrubber 16.
  • This gas mixture forms the reducing gas fed to the gas heater 18 and subsequently to the whirl layer reactors 1 to 4 and having the following composition:
  • the degree of metallization of the sponge iron is 92%.
  • the fine ore has the following analysis:
  • the reformed natural gas and the top gas have the chemical compositions indicated in the Table below.
  • the gas mixture emerging from the CO 2 scrubber 16 and formed of the scrubbed reformed natural gas and of the top gas has the following composition:
  • This gas mixture is mixed with 94,000 Nm 3 /h of top gas that has not been passed through the CO 2 scrubber 16.
  • This gas mixture forms the reducing gas fed to the gas heater 18 and subsequently to the whirl layer reactors 1 to 4 and has the following composition:
  • the degree of metallization of the sponge iron is 92%.
  • the invention is not limited to the above-described examples, but is applicable also to other direct reduction processes, for instance, such in which the whirl layer reactors 1 to 4 are replaced with shaft furnaces for lumpy ore.
  • the reformed natural gas also may be replaced with other reducing gases primarily containing CO and H 2 , such as

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  • Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Manufacturing & Machinery (AREA)
  • Materials Engineering (AREA)
  • Metallurgy (AREA)
  • Organic Chemistry (AREA)
  • Manufacture Of Iron (AREA)
  • Catalysts (AREA)
  • Manufacture And Refinement Of Metals (AREA)
US08/765,342 1994-06-23 1995-06-20 Process and plant for the direct reduction of iron-oxide-containing materials Expired - Fee Related US5871560A (en)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
AT0124894A AT402825B (de) 1994-06-23 1994-06-23 Verfahren zur direktreduktion von eisenoxidhältigem material
AT1248/94 1994-06-23
PCT/AT1995/000121 WO1996000302A1 (de) 1994-06-23 1995-06-20 Verfahren zur direktreduktion von eisenoxidhältigem material

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US (1) US5871560A (xx)
EP (1) EP0766747A1 (xx)
JP (1) JP3248915B2 (xx)
KR (1) KR100240811B1 (xx)
AT (1) AT402825B (xx)
AU (1) AU691293B2 (xx)
BR (1) BR9508108A (xx)
CA (1) CA2193855C (xx)
MX (1) MX9606728A (xx)
PE (1) PE49695A1 (xx)
RU (1) RU2125098C1 (xx)
UA (1) UA27080C2 (xx)
WO (1) WO1996000302A1 (xx)
ZA (1) ZA955177B (xx)

Cited By (16)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6136019A (en) * 1996-08-19 2000-10-24 Mower Family Chf Treatment Irrevocable Trust Augmentation of electrical conduction and contractility by biphasic cardiac pacing administered via the cardiac blood pool
WO2001011091A1 (en) * 1999-08-05 2001-02-15 Technological Resources Pty Ltd A direct smelting process
US6270553B1 (en) 1996-12-18 2001-08-07 Technological Resources Pty. Ltd. Direct reduction of metal oxide agglomerates
US6289034B1 (en) 1998-08-28 2001-09-11 Technologies Resources Pty. Ltd. Process and an apparatus for producing metals and metal alloys
US6328783B1 (en) 1996-12-18 2001-12-11 Technological Resources Pty Ltd Producing iron from solid iron carbide
US6379424B1 (en) 1999-10-26 2002-04-30 Technological Resources Pty. Ltd. Direct smelting apparatus and process
US6387153B1 (en) 1999-10-15 2002-05-14 Technological Resources Pty Ltd Stable idle procedure
US6423114B1 (en) 1999-08-10 2002-07-23 Technological Resources Pty. Ltd. Pressure control
US6428603B1 (en) 1999-09-27 2002-08-06 Technological Resources Pty., Ltd. Direct smelting process
US6517605B1 (en) 1999-07-09 2003-02-11 Technological Resources Pty. Ltd. Start-up procedure for direct smelting process
US6602321B2 (en) 2000-09-26 2003-08-05 Technological Resources Pty. Ltd. Direct smelting process
US20050277993A1 (en) * 1996-08-19 2005-12-15 Mower Morton M System and method for managing detrimental cardiac remodeling
US20080287855A1 (en) * 1996-08-19 2008-11-20 Mower Morton M System and method for managing detrimental cardiac remodeling
WO2008146112A1 (en) * 2007-05-25 2008-12-04 Hyl Technologies, S.A. De C.V Method and apparatus for the direct reduction of iron ores utilizing syngas
US20090133535A1 (en) * 2007-11-20 2009-05-28 Gijsbert Jan Van Heeringen Process for production of elemental iron
US7908003B1 (en) 1996-08-19 2011-03-15 Mr3 Medical Llc System and method for treating ischemia by improving cardiac efficiency

Families Citing this family (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
AT406382B (de) * 1996-11-06 2000-04-25 Voest Alpine Ind Anlagen Verfahren zum herstellen von eisenschwamm durch direktreduktion von eisenoxidhältigem material
US6149859A (en) † 1997-11-03 2000-11-21 Texaco Inc. Gasification plant for direct reduction reactors
KR100445835B1 (ko) * 2001-05-25 2004-08-25 한국타이어 주식회사 타이어 트레드용 고무 조성물
KR20030037530A (ko) * 2001-11-06 2003-05-14 박재석 일회용 전분제 용기 및 그 제조방법
CN109868335B (zh) * 2019-03-19 2021-01-26 重庆大学 一种闭环利用铁矿石还原过程中尾气的系统及方法

Citations (7)

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GB799551A (en) * 1956-02-06 1958-08-13 Texaco Development Corp Reduction of a metal oxide with carbon monoxide and hydrogen
US3936296A (en) * 1970-02-25 1976-02-03 Campbell Donald L Integrated fluidized reduction and melting of iron ores
DE2907022A1 (de) * 1979-02-23 1980-08-28 Maschf Augsburg Nuernberg Ag Tiefkuehl-aufbereitung von rohgas aus der kohlevergasung zur verwendung bei der direktreduktion
US4333761A (en) * 1979-10-22 1982-06-08 Midrex Corporation Method for direct reduction of iron using high sulfur gas
US4376648A (en) * 1980-12-04 1983-03-15 Mitsubishi Jukogyo Kabushiki Kaisha Process for producing reduced iron
EP0571358A1 (de) * 1992-05-22 1993-11-24 Voest-Alpine Industrieanlagenbau Gmbh Verfahren zur Direktreduktion von teilchenförmigem eisenoxidhältigen Material
US5531424A (en) * 1993-04-19 1996-07-02 Fior De Venezuela Fluidized bed direct reduction plant

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US3377156A (en) * 1965-07-30 1968-04-09 Exxon Research Engineering Co Process of reducing iron oxide ores with gases containing carbon monoxide

Patent Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB799551A (en) * 1956-02-06 1958-08-13 Texaco Development Corp Reduction of a metal oxide with carbon monoxide and hydrogen
US3936296A (en) * 1970-02-25 1976-02-03 Campbell Donald L Integrated fluidized reduction and melting of iron ores
DE2907022A1 (de) * 1979-02-23 1980-08-28 Maschf Augsburg Nuernberg Ag Tiefkuehl-aufbereitung von rohgas aus der kohlevergasung zur verwendung bei der direktreduktion
US4333761A (en) * 1979-10-22 1982-06-08 Midrex Corporation Method for direct reduction of iron using high sulfur gas
US4376648A (en) * 1980-12-04 1983-03-15 Mitsubishi Jukogyo Kabushiki Kaisha Process for producing reduced iron
EP0571358A1 (de) * 1992-05-22 1993-11-24 Voest-Alpine Industrieanlagenbau Gmbh Verfahren zur Direktreduktion von teilchenförmigem eisenoxidhältigen Material
US5531424A (en) * 1993-04-19 1996-07-02 Fior De Venezuela Fluidized bed direct reduction plant

Cited By (20)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6136019A (en) * 1996-08-19 2000-10-24 Mower Family Chf Treatment Irrevocable Trust Augmentation of electrical conduction and contractility by biphasic cardiac pacing administered via the cardiac blood pool
US8447399B2 (en) 1996-08-19 2013-05-21 Mr3 Medical, Llc System and method for managing detrimental cardiac remodeling
US7908003B1 (en) 1996-08-19 2011-03-15 Mr3 Medical Llc System and method for treating ischemia by improving cardiac efficiency
US20080287855A1 (en) * 1996-08-19 2008-11-20 Mower Morton M System and method for managing detrimental cardiac remodeling
US20060265017A9 (en) * 1996-08-19 2006-11-23 Mower Morton M System and method for managing detrimental cardiac remodeling
US20050277993A1 (en) * 1996-08-19 2005-12-15 Mower Morton M System and method for managing detrimental cardiac remodeling
US6270553B1 (en) 1996-12-18 2001-08-07 Technological Resources Pty. Ltd. Direct reduction of metal oxide agglomerates
US6328783B1 (en) 1996-12-18 2001-12-11 Technological Resources Pty Ltd Producing iron from solid iron carbide
US6289034B1 (en) 1998-08-28 2001-09-11 Technologies Resources Pty. Ltd. Process and an apparatus for producing metals and metal alloys
US6517605B1 (en) 1999-07-09 2003-02-11 Technological Resources Pty. Ltd. Start-up procedure for direct smelting process
KR100710724B1 (ko) * 1999-08-05 2007-04-24 테크놀라지칼 리소시스 피티와이. 리미티드. 금속을 함유하는 원료물질의 직접제련 방법
US6379422B1 (en) 1999-08-05 2002-04-30 Technological Resources Pty. Ltd. Direct smelting process
WO2001011091A1 (en) * 1999-08-05 2001-02-15 Technological Resources Pty Ltd A direct smelting process
US6423114B1 (en) 1999-08-10 2002-07-23 Technological Resources Pty. Ltd. Pressure control
US6428603B1 (en) 1999-09-27 2002-08-06 Technological Resources Pty., Ltd. Direct smelting process
US6387153B1 (en) 1999-10-15 2002-05-14 Technological Resources Pty Ltd Stable idle procedure
US6379424B1 (en) 1999-10-26 2002-04-30 Technological Resources Pty. Ltd. Direct smelting apparatus and process
US6602321B2 (en) 2000-09-26 2003-08-05 Technological Resources Pty. Ltd. Direct smelting process
WO2008146112A1 (en) * 2007-05-25 2008-12-04 Hyl Technologies, S.A. De C.V Method and apparatus for the direct reduction of iron ores utilizing syngas
US20090133535A1 (en) * 2007-11-20 2009-05-28 Gijsbert Jan Van Heeringen Process for production of elemental iron

Also Published As

Publication number Publication date
JPH10505634A (ja) 1998-06-02
CA2193855A1 (en) 1996-01-04
KR100240811B1 (ko) 2000-01-15
AT402825B (de) 1997-09-25
AU2556895A (en) 1996-01-19
EP0766747A1 (de) 1997-04-09
AU691293B2 (en) 1998-05-14
RU2125098C1 (ru) 1999-01-20
CA2193855C (en) 2001-09-18
BR9508108A (pt) 1997-08-12
UA27080C2 (uk) 2000-02-28
ZA955177B (en) 1996-01-31
JP3248915B2 (ja) 2002-01-21
MX9606728A (es) 1997-04-30
PE49695A1 (es) 1996-01-22
WO1996000302A1 (de) 1996-01-04
ATA124894A (de) 1997-01-15

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